EP0180599B1 - Membrane a flux eleve - Google Patents

Membrane a flux eleve Download PDF

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Publication number
EP0180599B1
EP0180599B1 EP85901918A EP85901918A EP0180599B1 EP 0180599 B1 EP0180599 B1 EP 0180599B1 EP 85901918 A EP85901918 A EP 85901918A EP 85901918 A EP85901918 A EP 85901918A EP 0180599 B1 EP0180599 B1 EP 0180599B1
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EP
European Patent Office
Prior art keywords
membrane
microskin
gel
molecules
substrate
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP85901918A
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German (de)
English (en)
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EP0180599A4 (fr
EP0180599A1 (fr
Inventor
Michel Serge Maxime Lefebvre
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Syrinx Research Pty Ltd
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Syrinx Research Pty Ltd
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Priority to AT85901918T priority Critical patent/ATE62148T1/de
Publication of EP0180599A1 publication Critical patent/EP0180599A1/fr
Publication of EP0180599A4 publication Critical patent/EP0180599A4/fr
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Publication of EP0180599B1 publication Critical patent/EP0180599B1/fr
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/12—Composite membranes; Ultra-thin membranes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D67/00—Processes specially adapted for manufacturing semi-permeable membranes for separation processes or apparatus
    • B01D67/0039—Inorganic membrane manufacture
    • B01D67/0048—Inorganic membrane manufacture by sol-gel transition
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
    • B01D71/02—Inorganic material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
    • B01D71/02—Inorganic material
    • B01D71/0213—Silicon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2323/00—Details relating to membrane preparation
    • B01D2323/48—Influencing the pH
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2325/00—Details relating to properties of membranes
    • B01D2325/08—Patterned membranes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2325/00—Details relating to properties of membranes
    • B01D2325/20—Specific permeability or cut-off range
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2325/00—Details relating to properties of membranes
    • B01D2325/30—Chemical resistance

Definitions

  • the present invention relates to a semi-permeable membrane having improved transmission properties (i.6. flux) useful inter alia for the industrial desalting of molasses or milk whey by ultrafiltration.
  • Ultrafiltration is used industrially for the recovery of valuable macro-molecular products, such as proteins. fats and viruses, for example in the recovery of protein from cheese whey.
  • ultrafiltration may be used in depollution applications, such as the removal of soluble oil from industrial waste effluents.
  • Typical biofilters have a pore size of about 0.1 to 1mm (10.000 angstrom) and can be used in connection with a filter aid (such as titanium oxide or alumina) which block the large pores of the biofilter to form a dynamic membrane.
  • the filter aid simply rests on the surface of the biofilter and is not attached in any way. Without this, the pore size produced is too large for ultrafiltration applications.
  • Membranes for biofiltration have been developed for particles as small as 0.08 mm (800 angstrom). Below these dimensions ultrafiltration membranes retain molecules with diameters as low as 1mm (10 angstrom) through a molecular sieve mechanism which in many respects is analogous to filtration.
  • Typical ultrafiltration membranes have pore dimensions in the range 1 to 20mm (10 to 200 angstrom).
  • ultrafiltration membranes have generally been formed of polymers, such as polyamides, polycarbonates and polysulphones.
  • the ultrafiltration membranes will be either in the form of flat sheet or tubular membranes, or in the form of hollow fibres.
  • organic polymeric systems suffers from a number of disadvantages.
  • the polymeric ultrafiltration membranes are chemically sensitive to extremes of pH and tend to be dissolved by a number of solvents. Since the manufacturing techniques generally involve phase inversion using a solution of the polymer, it is difficult to provide polymers which are sufficiently soluble to allow for ease of manufacture but are resistant to commonly encountered industrial solvents.
  • the total pore area of known ultrafiltration membranes is generally less than 10% of the total membrane surface area.
  • most commercially available ultrafiltration membranes at present on the market have a pore area less than 0.1% of the total membrane surface.
  • Such low porosity limits the flux of liquid which can pass through the membrane. It is possible to increase the flux by increasing the pressure differential across the membrane, but the maximum flux is limited in use by the build up of a layer of the separated macro-molecular species on the membrane. To minimise this build up, the membrane is subjected to a high rate of cross flow (i.e. a high shear rate) of the liquid being filtered.
  • a high shear rate i.e. a high shear rate
  • the present invention resides in the provision of a microskin having special properties on a macroporous substrate, such as a conventional biofilter.
  • the present invention provides a semi-permeable membrane for selective retention of molecules of greater than a pre-selected size having a macro-porous substrate, wherein a micro-porous microskin is deposited on the substrate, the microskin having a surface of Fractal geometry including means for generating a dynamic layer which is reticulated at the molecular level, including an ordered arrangement of adsorption/repulsion sites for said retained molecules of at least three different energy levels, the spacing between the adsorption and repulsion sites being of the same order of magnitude as the mean free path of Brownian motion of said retained molecules, wherein the microskin is formed of a desolvated gel selected so as to provide said at least three different energy levels.
  • Another aspect of the invention provides a method of preparing a semi-permeable membrane for selective retention of molecules of greater than a pre-selected size having a macro-porous substrate, comprising the steps of depositing a liquid-containing gel layer onto the substrate and removing liquid from the gel layer to produce a micro-porous microskin which is retained on the substrate, the microskin having a surface of Fractal geometry including means for generating a dynamic layer which is reticulated at the molecular level, including an ordered arrangement of adsorption/repulsion sites for said retained molecules of at least three different energy levels, the spacing between the adsorption and repulsion sites being of the same order of magnitude as the mean free path of Brownian motion of said retained molecules.
  • the invention also provides an ultrafiltration process using a membrane as described above.
  • the gel layer is treated to become permanently fixed on the substrate and is shrunk to develop a pleated reticulated Fractal surface.
  • the material of the microskin is chosen to have interactive properties with the molecules being retained to inhibit production of a flat monomolecular layer, and to generate a dynamic layer which is reticulated at the molecular level.
  • the membrane is useful for any membrane process which suffers from "gel-polarisation” (the formation of a layer of retained molecules which inhibits flux), particularly those driven by pressure, electric field or concentration gradient, such as ultrafiltration, reverse osmosis, electrodialysis, dialysis, and biofiltration.
  • the substrate itself does not constitute the membrane, the material of which it is formed is not critical.
  • the substrate material will be chosen bearing in mind the conditions under which the membrane will operate, and also the conditions required in the formation of the microskin.
  • the substrate may be formed of stainless steel or a ceramic material.
  • the substrate would preferably be formed of a ceramic material.
  • the substrate might be formed of an inert polymeric material, such as polypropylene. Such substrates are readily available as biofiltration materials.
  • the gel-layer may be produced of any suitable gelatinous material which can be converted to a permanent microskin on the surface of the porous substrate.
  • the gel may contain any polar solvent (e.g. liquid ammonia), usually the gel will be water-containing.
  • the gel will comprise a multivalent ion, especially a cation such as calcium, aluminium, arsenic. zirconium or silicon.
  • examples of gels include calcium apatite (usually prepared from milk whey), calcium aconitate (the calcium salt of propene-1,2,3- tricarboxylic acid) and calcium oxalate.
  • Carboxymethyl cellulose may also be used as a substrate additive.
  • the microskin is one with a Fractal surface.
  • a Fractal surface is one where any continuous curve drawn onto the surface is not differentiable at any point. Examples of natural phenomena exhibiting surfaces with Fractal geometry include snowflakes and elongated crystals. This property of continuity without differentiability has been observed for natural phenomena such as particle trajectories in quantum mechanics and Brownian motion.
  • a Fractal expression may be used to define certain porous media and highly heterogenous surfaces. A discussion of the application of Fractal expressions to transport properties is given in Le Mehaute and Crepy, Solid State Ionics 9 and 10 (1983) 17-30.
  • a reticulated Fractal surface whose dimensions of reticulation (spacing between adjacent adsorption and repulsion sites) are of the same order of magnitude as the Brownian motion of the molecules being filtered, leads to movement of molecules in the third dimension, thereby inhibiting production of a monomolecular layer and allowing increased flux.
  • a microskin whose filter transmission properties may be described by a Fractal expression
  • this may be achieved by using a gel formed from a tribasic compound such as calcium aconitate, aluminium hydroxide or phosphoric acid, which have three different replaceable groups (e.g. hydrogen or hydroxyl) of the same type but different energy levels.
  • the three different energy levels lead to the three-dimensional reticulated Fractal structure when liquid is removed from the gel.
  • the reticulated structure is generated by the molecular rearrangement caused by removal of liquid from the gel.
  • the Fractal surface is characterised by not polarising light and by exhibiting an angular structure when viewed under the microscope.
  • the gel layer is built up by passing a colloid of the material over the porous substrate.
  • a high shear rate is used.
  • the shear rate is preferably in excess of 2000 s ⁇ 1 .
  • the shear rate is proportional to the velocity divided by the channel width in the case of a hollow fibre.
  • the porosity of the final microskin depends on the amount of liquid included in the gel. Thus, high degrees of hydration lead to larger pore sizes and vice versa.
  • the liquid may be removed from the gel layer by any suitable chemical or physical process.
  • the liquid may be removed partially or completely.
  • liquid may be removed by change of pH, oxidation. hydrolysis or denaturation.
  • the structure of the calcium salts of aconitic acid depends on pH. Water can be gradually dislodged from the gel by progressively changing the pH.
  • the gel layer is subjected to a high pressure differential during dehydration so as to compact the layer.
  • the dehydration treatment will be sufficient to permanently fix the microskin to the substrate.
  • Such transformations may include the chemical and physical treatments discussed above.
  • this may be subjected to a carbonizing process at very high temperatures, for example using a plasma.
  • membranes having a high flux may be produced.
  • the membranes may be arranged to have a low tendency to poisoning, to be resistant to extremes of temperature, and to be inert to extremes of chemical conditions. such as pH and solvents.
  • Figure 1 is a schematic cross-section of an ultrafiltration tube which comprises a polycarbonate jacket 1 enclosing a bundle 2 of hollow fibres potted at either end into the jacket using polyurethane potting compound 3.
  • End caps 4 and 5 are attached to the jacket by silicone washers 6 and 7, and are each provided with connectors 8 and 9 for attaching feed inlet and outlet tubes respectively.
  • the jacket is provided with an outlet 10 for permeate which has passed through the ultrafiltration fibres.
  • An outlet 11 provided with a removable screw cap 12 is provided for use during back-flushing of the filter.
  • a "Fractal tube” was prepared as follows.
  • a polypropylene biofilter (see Figure 1) comprising an assembly of 2000 hollow fibres, having an effective area of 0.4 m2 a fibre internal diameter of 313 ⁇ m, a fibre length of 185 mm and a pore size of 0.45 ⁇ m was cleaned by passing distilled water at 50°C at a pressure drop of 150 kPa through the filter to remove plasticiser. After a half an hour the flux had stabilised indicating completion of the cleaning.
  • a solution comprising a mixture of 0.5 wt % calcium aconitate and 0.5 wt % calcium oxalate salts at 35°C was then passed through the filter at a pressure drop of 150 kPa for 30 minutes at a cross flow rate of 4 litres per minute.
  • the total concentration of the solution was gradually increased from 1 wt % to 8 wt %.
  • the pH of the solution was then adjusted using sulphuric acid to a pH of 3.6 so as to dehydrate and transform the calcium aconitate gel layer to a Fractal surface.
  • the filter was then cleaned with Pyroneg (trade mark) a commercial formulation including surfactant, oxidiser and bacteriostats) to produce the finished ultrafiltration membrane.
  • the ultrafiltration membrane was found to have a flux of 3 to 5 times higher than conventional polyamide membranes of similar molecular weight cut-off.
  • the membrane showed excellent chemical resistance and could be heated to high temperatures.
  • a "Fractal tube” having a calcium apatite microskin was prepared using an analogous procedure to Example 1.
  • Milk whey was acidified to pH 4.6 to precipitate casein. Phosphoric acid was then added to bring the pH down to 2 and to convert the casein to a calcium apatite colloid. The colloid was then passed through the stabilised biofilter tubes to deposit it as a gel on the filter surface.
  • the microskin was reticulated and permanently fixed to the filter surface by addition of calcium hydroxide to change the pH to 7 and to partially dehydrate the calcium apatite gel.
  • the cleaned ultrafiltration membrane exhibited a three-fold increase in flux compared to conventional polyamide-imide membranes.
  • the controls are polyamide-imide membranes having an amphoteric dyestuff grafted on.
  • the physical dimensions are as follows:
  • the major limitation of such a process is the low flux shown by conventional membranes, when operating on viscous molasses feeds at economically viable brix (a measure of viscosity) levels. Evaporation, required to reconcentrate the product for storage, and optimisation of calcium elimination have considerable repercussions on economics.
  • the performance of the Fractal membrane P1 was compared to the control D31 by monitoring the flux and calcium rejection characteristics at various levels of molasses feed viscosity. During the trial a snap sample was taken of the feed and permeate from each tube, and analysed for calcium content. At this point the feed brix was 33° with a pH of 5.35, a temperature of 20° C, and ultrafiltration pressures inlet and outlet of 150 kPa and 50 kPa respectively. Calcium determinations showed a somewhat similar rejection for each membrane. The removal level for the control was 19.6%, and for the Fractal membrane, 17.9%.
  • the flux/viscosity plot of Figure 2 depicts the superiority of the Fractal tube (P1).
  • the flux profile at 8°C is shown in Figure 5.
  • the Fractal tube outperforms the control by a factor of two.
  • Figure 6 shows the flux decline with time for two Fractal tubes P1 and P2 in comparison with a control D31 in the ultrafiltration of effluent from a flour mill.
  • the effluent contains 0.85 wt% solids comprised mainly of protein and sugars.
  • the flux of the Fractal tubes is at least twice that of the control.

Claims (15)

  1. Membrane semi-perméable destinée à la rétention sélective de molécules de taille supérieure à une taille présélectionnée, possédant un substrat macroporeux, dans laquelle une micropellicule microporeuse est déposée sur le substrat, la micropellicule ayant une surface de géométrie fractale comprenant des moyens de génération d'une couche dynamique qui est réticulée au niveau moléculaire, comprenant un arrangement ordonné des sites d'adsorption/ répulsion pour lesdites molécules retenues d'au moins trois niveaux d'énergie différents, la distance entre les sites d'adsorption et de répulsion étant du même ordre de grandeur que le parcours libre moyen du mouvement brownien desdites molécules retenues, dans laquelle la micropellicule est en un gel dissous sélectionné de façon à fournir lesdits niveaux d'énergie différents qui sont au minimum au nombre de trois.
  2. Membrane selon la revendication 1, dans laquelle la distance de réticulation est comprise dans la plage de 0,1 à 2 nm (1 à 20 Å).
  3. Membrane selon la revendication 1 ou la revendication 2, dans laquelle la micropellicule comprend un composé d'un ion multivalent.
  4. Membrane selon la revendication 3, dans laquelle la micropellicule comprend un composé tribasique.
  5. Membrane selon la revendication 4, dans laquelle un cation du composé tribasique est sélectionné parmi le calcium, l'aluminium, le phosphore et le silicium.
  6. Membrane selon la revendication 5, dans laquelle la micropellicule comprend de l'apatite de calcium.
  7. Membrane selon la revendication 5, dans laquelle la micropellicule comprend de l'aconitate de calcium.
  8. Procédé de préparation d'une membrane semi-perméable destinée à la rétention sélective de molécules de taille supérieure à une taille présélectionnée, possédant un substrat macroporeux, comprenant les étapes de dépôt d'une couche de gel contenant un liquide sur le substrat et d'enlèvement du liquide de la couche de gel pour produire une micropellicule microporeuse qui est retenue sur le substrat, la micropellicule ayant une surface de géométrie fractale comprenant des moyens de génération d'une couche dynamique qui est réticulée au niveau moléculaire, comprenant un arrangement ordonné des sites d'adsorption/répulsion pour lesdites molécules retenues d'au moins trois niveaux d'énergie différents, la distance entre les sites d'adsorption et de répulsion étant du même ordre de grandeur que le parcours libre moyen du mouvement brownien desdites molécules retenues.
  9. Procédé selon la revendication 8, dans lequel le gel comprend de l'apatite de calcium hydratée.
  10. Procédé selon la revendication 8, dans lequel le gel comprend de l'aconitate de calcium hydraté.
  11. Procédé selon l'une quelconque des revendications 8 à 10, dans lequel la couche de gel est formée par passage d'un colloïde sur le substrat poreux.
  12. Procédé selon la revendication 11, dans lequel le colloïde est passé sur le substrat poreux pour un gradient de cisaillement supérieur à 2 000 s⁻¹.
  13. Procédé selon l'une quelconque des revendications 8 à 12, dans lequel le liquide est retiré du gel par modification du pH.
  14. Procédé selon l'une quelconque des revendications 8 à 12, dans lequel le liquide est retiré du gel par traitement thermique.
  15. Procédé d'ultrafiltration, dans lequel est utilisée une membrane selon l'une quelconque des revendications 1 à 7.
EP85901918A 1984-04-11 1985-04-10 Membrane a flux eleve Expired - Lifetime EP0180599B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT85901918T ATE62148T1 (de) 1984-04-11 1985-04-10 Membran mit hohem flux.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU4531/84 1984-04-11
AUPG453184 1984-04-11

Publications (3)

Publication Number Publication Date
EP0180599A1 EP0180599A1 (fr) 1986-05-14
EP0180599A4 EP0180599A4 (fr) 1988-05-03
EP0180599B1 true EP0180599B1 (fr) 1991-04-03

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EP85901918A Expired - Lifetime EP0180599B1 (fr) 1984-04-11 1985-04-10 Membrane a flux eleve

Country Status (12)

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US (1) US4749487A (fr)
EP (1) EP0180599B1 (fr)
JP (1) JPS61501830A (fr)
AT (1) ATE62148T1 (fr)
AU (1) AU576364B2 (fr)
DE (1) DE3582394D1 (fr)
DK (1) DK571085A (fr)
IL (1) IL74884A0 (fr)
IN (1) IN165125B (fr)
NZ (1) NZ211755A (fr)
WO (1) WO1985004593A1 (fr)
ZA (1) ZA852711B (fr)

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HUE061765T2 (hu) 2013-10-02 2023-08-28 Rohm & Haas Electronic Mat Singapore Pte Ltd Berendezés membrán filtrációs modul javítására
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Also Published As

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WO1985004593A1 (fr) 1985-10-24
IL74884A0 (en) 1985-07-31
JPS61501830A (ja) 1986-08-28
EP0180599A4 (fr) 1988-05-03
AU4291585A (en) 1985-11-01
DK571085D0 (da) 1985-12-10
AU576364B2 (en) 1988-08-25
IN165125B (fr) 1989-08-19
EP0180599A1 (fr) 1986-05-14
US4749487A (en) 1988-06-07
NZ211755A (en) 1987-11-27
DK571085A (da) 1985-12-10
DE3582394D1 (de) 1991-05-08
ATE62148T1 (de) 1991-04-15
ZA852711B (en) 1985-12-24

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